EP4077898B1 - Energy conversion system - Google Patents

Energy conversion system Download PDF

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Publication number
EP4077898B1
EP4077898B1 EP20799724.8A EP20799724A EP4077898B1 EP 4077898 B1 EP4077898 B1 EP 4077898B1 EP 20799724 A EP20799724 A EP 20799724A EP 4077898 B1 EP4077898 B1 EP 4077898B1
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Prior art keywords
unit
sofc
energy conversion
conversion system
oxidant
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German (de)
English (en)
French (fr)
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EP4077898A1 (en
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Emanuele Martelli
Stefano Campanari
Manuele Gatti
Roberto SCACCABAROZZI
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Eni SpA
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Eni SpA
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    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
    • H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
    • H01M8/0618—Reforming processes, e.g. autothermal, partial oxidation or steam reforming
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C1/00—Gas-turbine plants characterised by the use of hot gases or unheated pressurised gases, as the working fluid
    • F02C1/04—Gas-turbine plants characterised by the use of hot gases or unheated pressurised gases, as the working fluid the working fluid being heated indirectly
    • F02C1/08—Semi-closed cycles
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
    • F02C3/34—Gas-turbine plants characterised by the use of combustion products as the working fluid with recycling of part of the working fluid, i.e. semi-closed cycles with combustion products in the closed part of the cycle
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
    • H01M8/04014—Heat exchange using gaseous fluids; Heat exchange by combustion of reactants
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
    • H01M8/04014—Heat exchange using gaseous fluids; Heat exchange by combustion of reactants
    • H01M8/04022—Heating by combustion
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
    • H01M8/04067—Heat exchange or temperature measuring elements, thermal insulation, e.g. heat pipes, heat pumps, fins
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
    • H01M8/04089—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
    • H01M8/04097—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with recycling of the reactants
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
    • H01M8/04201—Reactant storage and supply, e.g. means for feeding, pipes
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
    • H01M8/0668—Removal of carbon monoxide or carbon dioxide
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/10—Fuel cells with solid electrolytes
    • H01M8/12—Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F05—INDEXING SCHEMES RELATING TO ENGINES OR PUMPS IN VARIOUS SUBCLASSES OF CLASSES F01-F04
    • F05D—INDEXING SCHEME FOR ASPECTS RELATING TO NON-POSITIVE-DISPLACEMENT MACHINES OR ENGINES, GAS-TURBINES OR JET-PROPULSION PLANTS
    • F05D2260/00—Function
    • F05D2260/60—Fluid transfer
    • F05D2260/61—Removal of CO2
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/10—Fuel cells with solid electrolytes
    • H01M8/12—Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte
    • H01M2008/1293—Fuel cells with solid oxide electrolytes
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M2250/00—Fuel cells for particular applications; Specific features of fuel cell system
    • H01M2250/40—Combination of fuel cells with other energy production systems
    • H01M2250/407—Combination of fuel cells with mechanical energy generators
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/50—Fuel cells

Definitions

  • the present invention refers to an energy conversion system, which converts gaseous fuels into electricity.
  • the Allam cycle is an oxy-combustion cycle in which a combination of pure oxygen and methane, natural gas or syngas is burnt at high pressure using a large flow rate of recycled CO 2 as temperature moderator.
  • the combustor working pressure is "supercritical" and a regenerator is used to preheat the recycled stream.
  • the Allam cycle is reported to be able to achieve a 55 - 60 % net electric efficiency with 100 % CO 2 capture.
  • the cycle operates with a turbine inlet temperature of 1100 - 1300 °C (1373-1573 K) (requiring blade cooling and directionally-solidified superalloys) and a regenerator inlet temperature of 650 - 750 °C (923-1023K) (requiring special alloys, like Ni-based alloy materials such as Inconel 617).
  • gaseous fuels for example, but not limited to, natural gas, syngas, biogas, biomethane, light hydrocarbons, hydrogen
  • liquid fuels for example, but not limited to, light hydrocarbons, alcohol, methanol, DME
  • the idea underlying the invention consists of providing a system, which integrates a Solid Oxide Fuel Cell (SOFC) unit working in pressurized conditions up to high pressures (5 - 500 bar) with a semi-closed oxy-combustion cycle, which uses the heat and the unconverted fuel and oxidant streams discharged by the fuel cell.
  • SOFC Solid Oxide Fuel Cell
  • the oxy-combustion cycle is a semi-closed Brayton cycle featuring CO 2 as the main working fluid. If the SOFC unit working pressure is above the critical one, the Brayton cycle becomes a supercritical CO 2 cycle. Although with lower efficiency, the system can also work with maximum cycle pressures below the CO 2 critical one (73.8 bar). Thus, the CO 2 stream is the working fluid of both the thermodynamic cycle and the SOFC unit.
  • Another peculiarity of the system is the use of the unconverted O 2 discharged by the SOFC unit within the combustor of the semi-closed Brayton cycle.
  • the system is referred to as " Solid Oxide Semi-closed CO 2 cycle - SOSCO2 ".
  • An advantage of the present system is that the power plant has zero emissions of pollutants and greenhouse gases, if the separated CO 2 stream is captured and stored.
  • the claimed system can achieve net electric efficiencies (LHV basis) higher than conventional technologies (75 % compared to 55 - 62 % of natural gas combined cycles and 55 - 60 % of the Allam cycle) thanks to the optimized integration with the SOFC unit.
  • the present system has a superior operational flexibility (i.e., more independent operative variables) compared to conventional gas turbine cycles, as it likely allows achieving higher part-load efficiency and lower minimum turndown ratio.
  • Such operational flexibility is a very important feature for todays and future power plants due to the increasing penetration of intermittent renewables in the electric grid.
  • the present system provides a higher net electric efficiency (75 % vs. 55 - 60 %) which cannot be achieved by the Allam cycle and similar oxy-turbine cycles even using the most advanced gas turbine materials, such as advanced single crystal super alloys.
  • the operating conditions of the turbine are considerably less severe and suitable for uncooled turbines.
  • the turbine has an inlet temperature of 1100 - 1250 °C (1373-1523K).
  • the claimed system can achieve close-to-optimal efficiency with turbine inlet temperatures of 800 - 900 °C (1073-1173K), temperatures suitable for uncooled expander units and less expensive materials (more conventional super-alloys, avoiding the necessity of directionally solidified and single crystal blades), and slightly higher efficiency (with up to 1 % increase) with turbine inlet temperatures of 1000 - 1100 °C (1273-1373K) with limited cooling.
  • Very high efficiencies, above 70 % can be achieved even using an uncooled expander featuring an inlet temperature below 900 °C (1173K).
  • the optimal turbine outlet temperature is in the range 400 - 600 °C (673-873K), which are also here compatible with less costly materials (e.g., medium-high grade steel, ferritic stainless steels or conventional austenitic stainless steels).
  • the turbine discharges at temperatures in the range 650 - 750 °C (923-1023K), making it necessary to use very expensive nickel-based alloys (e.g., Inconel 617).
  • the combustor operates with lower thermal duty (the majority of fuel chemical energy is converted into the fuel cell) and lower maximum temperatures, corresponding to the turbine inlet conditions, with respect to the Allam cycle.
  • FIGS 1-3 show embodiments of an energy conversion system and parts thereof according to the invention.
  • the energy conversion system according to the invention comprises:
  • the energy conversion system comprises a high-pressure Solid Oxide Fuel Cell (SOFC) A with a semi-closed oxy-combustion Brayton cycle using CO 2 as moderator of the combustion temperature.
  • SOFC Solid Oxide Fuel Cell
  • the maximum cycle pressure and the SOFC unit A operating pressure are preferably above the critical pressure of CO 2 (i.e., > 73.9 bar).
  • the semi-closed Brayton cycle is a supercritical CO 2 cycle with advantages in terms of efficiency.
  • the energy conversion system can use either a gaseous or a liquid fuel 1.
  • the fuel shall be pressurized, optionally preheated, then is fed to the anode of the SOFC unit A while the oxidant mixture containing CO 2 and O 2 4, preheated in a regenerative heat exchanger D , is fed to the SOFC cathode side.
  • the SOFC unit A can be designed to run either with or without internal reforming (e.g., adopting specific catalysts, such as Ni-based materials typically used for commercially available SOFCs ), depending on the type of fuel to be used; in the case of natural gas feeding, methane is converted into hydrogen within the cell according to the reactions of steam reforming and water gas shift:
  • the reforming reaction which is highly endothermic, occurs exploiting available heat from the cell losses (thus converting heat into chemical energy, with an advantage for the system electric efficiency) and is driven by the consumption of hydrogen allowed by the electrochemical reactions (Eq. 1,2).
  • Steam required for hydrocarbons reforming can be supplied directly stream 3 and/or through recycling a fraction of the stream exiting the anode 40.
  • an ejector (O) or a fan X capable of withstanding high gas temperatures can provide the pressure head required to sustain the stream recycle.
  • the compressed fuel entering the power plant can therefore be mixed with part of the stream recycled from the anode outlet 40 and/or with steam 3 (which can be generated in the heat exchanger D ). Then, the stream entering the anode side can be preheated within the SOFC unit A to the final operating temperature (e.g., 700 - 850 °C) using the thermal power made available by the electrochemical process, through either a dedicated heat exchanger P (e.g., cooling the product streams) or internally in the fuel cell stack.
  • a dedicated heat exchanger P e.g., cooling the product streams
  • the SOFC unit can be fed directly with methane without needing a preliminary mixing with steam or recycled anode exhaust.
  • the unconverted fuel and oxygen leaving the SOFC unit A are sent to the combustor unit B of the semi-closed cycle.
  • the combustor unit B of the semi-closed cycle.
  • the combustion products 10 are mainly CO 2 and H 2 O, and may contain also some amounts of O 2 , Ar, N 2 and other chemical species.
  • the product gases are expanded in an expander C to a lower pressure, indicatively in the range 1 - 50 bar.
  • a lower pressure indicatively in the range 1 - 50 bar.
  • such value depends on the other pressures and temperatures of the cycle, and it may not be limited to such range.
  • the turbine inlet temperature can be higher or lower, requiring to adopt a cooled or uncooled expander C.
  • the cooling flows 11 can be taken from the stream of recycled CO 2 and can be preheated in the regenerator D.
  • the product gases 10 leaving the turbine are cooled in the regenerator D and then in a cooler E to a temperature approaching that of the heat sink (e.g., lake, river, sea, air, cold streams of other plants).
  • Most of the H 2 O of the product gases condenses, and it is separated with a gas-liquid separator F , such as a flash drum.
  • the outlet gas stream leaving the separator 16 is rich in CO 2 .
  • a fraction can be recycled 18 to be used as temperature moderator and/or to be mixed with the oxygen stream 21 and/or used as turbine cooling flow 11 while the remaining part 17 can be separated and either vented into the atmosphere or sent to the CO 2 purification and utilization/storage system.
  • compressing the recycle CO 2 -rich stream above the critical pressure if water condenses, it is possible to use a liquid-liquid separation process to remove further water.
  • CO 2 purification unit a conventional plant capable of producing nearly pure liquid CO 2 .
  • regenerator D It is also possible to recover heat in the regenerator D from the main compressor of the Air Separation Unit (ASU) and/or the intercoolers of the compressors H,K,L and/or from nearby heat sources. This can result in a further improvement of the efficiency of the proposed energy conversion system.
  • ASU Air Separation Unit
  • Table 1 indicative ranges of operating pressures and temperatures for the key streams.
  • Type of parameter Operating range Working pressure of the SOFC (A) and combustor (B) units 5 - 500 bar Expander (C) outlet pressure 1 - 50 bar
  • a second oxidation stage after the expansion (reheating configuration), adding a second SOFC unit AF and/or a second combustor unit AG optionally feeding additional fuel 61 and oxidant 62.
  • the working fluid can be further expanded in a second expander AH before entering the regenerator AI (see Figure 3 ).
  • This scheme can further increase the power output of the plant and lead to a lower specific investment cost (total plant cost / net electric power), specially for designs featuring one SOFC, two combustors and two expanders.
  • This second embodiment could also feature a wider operational range thanks to the possibility of adjusting the fuel flow rate fed to the different SOFCs and/or combustors.
  • Fuel is a natural gas with composition reported in Table 2: Table 2 - Composition of the fuel considered in the simulation example Type of molecule Composition, molar basis CH 4 89.00 % C 2 H 6 7.00 % C 3 H 8 1.00 % i-C 4 H 10 0.05 % n-C 4 H 10 0.05 % i-C 5 H 12 0.005 % n-C 5 H 12 0.005 % CO 2 2.00 % N 2 0.89 % - The oxygen is provided at 120 bar and 15 °C (288K), thus compressor H pressurizes stream 19 to 120 bar.
  • - Stream 2 is liquid water at 15 °C (288K), 1.013 bar.
  • the proposed system still can be designed and operated in a large variety of conditions due to the possibility of varying (i) the SOFC A unit and combustor B operative pressure, (ii) the expander C outlet pressure, (iii) the fraction of the unconverted fuel 40 recycled back to the anode inlet, (iv) the mass flow rate of the temperature moderator 9 of the combustor, (v) the regenerator outlet temperature of the oxidant 26 , temperature moderator 9 and steam 3 , (vi) the regenerator outlet temperature of the expander cooling flows 11 , and (vii) the fraction of the recycled 20 stream mixed with the oxygen to produce the oxidant flow.
  • the above listed independent variables have been optimized using a systematic process optimization approach.
  • the objective function to be maximized is the net electric efficiency (net electric power output of the integrated system divided the chemical power of the inlet fuel, LHV basis).
  • the optimization constraints considered in this example are summarized in Table 3: Table 3 - Technical constraints considered in the optimization example.
  • Parameter Value Concentration of oxygen at the SOFC cathode outlet (35) % mol (minimum) 10 % mol Concentration of water at the SOFC anode outlet (34) (maximum) 60 % mol
  • Temperature difference within the regenerator (D) (minimum) 5 °C Temperature difference at the hot end of the regenerator (D) (min- imum) 20 °C Expander (C) allowed metal temperature (maximum) 860 °C C/O at the SOFC (A) anode inlet 2.5 -
  • the oxidant, the temperature moderator and the steam for the SOFC unit exit the regenerator at the same temperature. Moreover, it is assumed that the oxidant provides 3 % excess of oxygen compared to the stoichiometric condition.
  • the optimization problem has been tackled using an optimization algorithm specifically developed for process and energy system optimization purposes.
  • the SOFC produces 72.7 % of the plant gross power output while the turbine accounts for the remaining 27.3 %.
  • the intercooled compression and the ASU are the two major penalties, consuming 5.5 % and 12.0 % of the gross power output respectively.
  • the resulting net electric efficiency is 76.2 % without CO 2 capture (i.e., venting the excess CO 2 not recycled), and 75.4 % with CO 2 capture.
  • the resulting performance indexes are outstanding compared to state-of-the-art as well as advanced energy systems (with and without CO 2 capture) which feature efficiencies in the range 60 - 63 % for the systems without capture, and 40 - 46 % for the systems with capture.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Sustainable Development (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Sustainable Energy (AREA)
  • Manufacturing & Machinery (AREA)
  • Electrochemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Fuel Cell (AREA)
EP20799724.8A 2019-12-16 2020-11-05 Energy conversion system Active EP4077898B1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
HRP20241009TT HRP20241009T1 (hr) 2019-12-16 2020-11-05 Sustav pretvorbe energije

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IT102019000024162A IT201900024162A1 (it) 2019-12-16 2019-12-16 Sistema di conversione di energia
PCT/EP2020/081054 WO2021121762A1 (en) 2019-12-16 2020-11-05 Energy conversion system

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EP4077898A1 EP4077898A1 (en) 2022-10-26
EP4077898B1 true EP4077898B1 (en) 2024-06-19

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US (1) US20230030209A1 (pl)
EP (1) EP4077898B1 (pl)
DK (1) DK4077898T3 (pl)
ES (1) ES2986608T3 (pl)
HR (1) HRP20241009T1 (pl)
HU (1) HUE067025T2 (pl)
IT (1) IT201900024162A1 (pl)
PL (1) PL4077898T3 (pl)
WO (1) WO2021121762A1 (pl)

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Publication number Priority date Publication date Assignee Title
WO2020101929A1 (en) * 2018-11-14 2020-05-22 Precision Combustion, Inc. Integrated power generation system
CN116706123A (zh) 2023-07-24 2023-09-05 江苏科技大学 基于阴极与阳极再循环的sofc/gt/sco2混合动力系统

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DE50115748D1 (de) * 2000-10-13 2011-02-03 Alstom Technology Ltd Verfahren zum Betrieb einer Kraftwerksanlage
US6868677B2 (en) * 2001-05-24 2005-03-22 Clean Energy Systems, Inc. Combined fuel cell and fuel combustion power generation systems
US7067208B2 (en) * 2002-02-20 2006-06-27 Ion America Corporation Load matched power generation system including a solid oxide fuel cell and a heat pump and an optional turbine
US7118818B2 (en) * 2002-10-01 2006-10-10 Rolls-Royce Plc Solid oxide fuel cell system
US7306871B2 (en) 2004-03-04 2007-12-11 Delphi Technologies, Inc. Hybrid power generating system combining a fuel cell and a gas turbine
US7709118B2 (en) 2004-11-18 2010-05-04 Siemens Energy, Inc. Recuperated atmospheric SOFC/gas turbine hybrid cycle
CA2595880A1 (en) * 2005-01-25 2006-08-03 Nuvera Fuel Cells, Inc. Fuel cell power plants
US7743861B2 (en) * 2006-01-06 2010-06-29 Delphi Technologies, Inc. Hybrid solid oxide fuel cell and gas turbine electric generating system using liquid oxygen
US7862938B2 (en) * 2007-02-05 2011-01-04 Fuelcell Energy, Inc. Integrated fuel cell and heat engine hybrid system for high efficiency power generation
WO2011001311A2 (en) 2009-07-03 2011-01-06 Ecole Polytechnique Federale De Lausanne (Epfl) Hybrid cycle sofc - inverted gas turbine with co2 separation
GB2494667A (en) * 2011-09-15 2013-03-20 Rolls Royce Fuel Cell Systems Ltd A solid oxide fuel cell system
JP6125224B2 (ja) * 2012-12-25 2017-05-10 三菱日立パワーシステムズ株式会社 発電システム及び発電システムの運転方法

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WO2021121762A1 (en) 2021-06-24
IT201900024162A1 (it) 2021-06-16
HRP20241009T1 (hr) 2024-11-08
DK4077898T3 (da) 2024-07-01
US20230030209A1 (en) 2023-02-02
ES2986608T3 (es) 2024-11-12
HUE067025T2 (hu) 2024-09-28
EP4077898A1 (en) 2022-10-26
PL4077898T3 (pl) 2024-10-07

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